Process for producing olefin polymers and catalyst used therein

ABSTRACT

Olefin polymers are produced by a process which comprises homopolymerizing or copolymerizing olefins in the presence of a catalyst system comprising: 
     (A) a solid catalyst component containing a trivalent titanium compound, which is obtained by reducing a titanium compound represented by the general formula Ti(OR 1 ) n  X 4-n  (wherein R 1  is a hydrocarbon group having 1 to 20 carbon atoms, X is a halogen atom and n is a number satisfying 0&lt;n≦4) with an organo magnesium compound and then treating the resulting solid product with a mixture of an ether compound and titanium tetrachloride, and 
     (B) an organo aluminum compound. 
     The above-mentioned reducing of a titanium compound with an organo magnesium compound may be performed in the presence of an organo silicon compound having Si-O bonds.

This is a division of application Ser. No. 872,900, filed June 11, 1986and now U.S. Pat. No. 4,771,023.

BACKGROUND OF THE INVENTION

1. Field of the Invention

This invention relates to a catalyst for producing olefin polymers, aswell as to a process for producing olefin polymers using said catalyst.More particularly, the present invention relates to (1) a solid catalystcomponent having very high catalytic activities not only per transitionmetal but also per solid catalyst in various polymerization process(e.g. slurry polymerization, gas phase polymerization, high temperaturesolution polymerization, high pressure ionic polymerization), (2) acatalyst system using said solid catalyst component and (3) a processfor producing olefin polymers using said catalyst system.

Use of a high activity catalyst in production of olefin polymers has avery high industrial value because it requires no removal of catalystresidue from olefin polymers produced and can provide a simplifiedprocess for producing olefin polymers. It is necessary that this highactivity catalyst has high catalytic activities not only per transitionmetal but also per solid catalyst.

When a metal halide such as titanium halide, magnesium halide or thelike is used in solid catalysts, high catalytic activity per solidcatalyst is necessary also from the standpoint of countermeasures whichmust be taken for corrosion of equipments and apparatuses caused byactive halogen.

2. Description of the Prior Art

Catalysts consisting of a transition metal compound (e.g. titaniumtetrachloride) supported by a carrier (e.g. a magnesium compound) haverecently been developed. These catalysts have higher catalyticactivities than conventional catalysts but are not satisfactory incatalytic activity per solid catalyst (Belgium Pat. No. 759601, JapanesePatent Publication No. 46269/1972, Japanese Patent Publication No.26383/1972, etc.).

As catalyst systems using a solid product obtained by reducing atitanium compound with an organo magnesium compound, there are disclosedsolid catalyst components consisting of a Grignard reagent and titaniumtetrachloride or an alkoxy-containing titanium halide [Japanese patentapplication Kokai (Laid-open) No. 4391/1971, Japanese Patent PublicationNo. 40959/1972, Japanese Patent Publication No. 39470/1975, U.S. Pat.No. 3,917,575, etc.], as well as solid catalyst components obtained byreacting a Grignard reagent with an alkoxy-containing titanium halideand then treating the resulting reaction product with titaniumtetrachloride [Japanese Patent Publication No. 24361/1972, Japanesepatent application Kokai (Laid-open) No. 115302/1971, etc.]. However,these solid catalyst components are not satisfactory in catalyticactivities per transition metal and also per solid catalyst component.

SUMMARY OF THE INVENTION

Under such circumstances, the objects of the present invention reside inproviding (1) a solid catalyst component having such high catalyticactivities not only per transition metal but also per solid catalystcomponent as making the removal of catalyst residue unnecessary, (2) acatalyst system using said solid catalyst component and (3) a processfor producing olefin polymers using said catalyst system.

According to the present invention, there are provided:

(I) a solid catalyst component (A) containing a tri-valent titaniumcompound, which is obtained by reducing a titanium compound representedby the general formula Ti(OR¹)_(n) X_(4-n) (wherein R¹ is a hydrocarbongroup having 1 to 20 carbon atoms, X is a halogen atom and n is a numbersatisfying 0<n≦4) with an organo magnesium compound and then treatingthe resulting solid product with a mixture of an ether compound andtitanium tetrachloride,

(II) a catalyst system consisting of said solid catalyst component (A)and an organo alumium compound (B), and

(III) a process for homoplymerizing or copolymerizing olefins using saidcatalyst system.

DETAILED DESCRIPTION OF THE INVENTION

The present invention will be explained specifically below.

The titanium compound used in the present invention is represented bythe general formula Ti(OR¹)_(n) X_(4-n) (wherein R¹ is a hydrocarbongroup of 1 to 20 carbon atoms; X is a halogen atom; and n is a numbersatisfying 0<n≦4). Specific examples of R¹ include alkyl groups such asmethyl, ethyl, n-propyl, isopropyl, n-butyl, isobutyl, n-amyl, isoamyl,n-hexyl, n-heptyl, n-octyl, n-decyl, n-dodecyl and the like; aryl groupssuch as phenyl, cresyl, xylyl, naphthyl and the like; cycloalkyl groupssuch as cyclohexyl, cyclopentyl and the like; alkenyl groups such aspropenyl and the like; and aralkyl groups such as benzyl and the like.

As the R¹, an alkyl group of 2 to 18 carbon atoms or an aryl group of 6to 18 carbon atoms is preferred. A straight chain alkyl group of 2 to 18carbon atoms is particularly preferred.

It is possible to use a titanium compound having two or more different--OR¹ groups.

As the halogen atom represented by X, there can be used chlorine,bromine, iodine or the like. Of these, chlorine gives a most desirableresult.

The n of the general formula Ti(OR¹)_(n) X_(4-n) is a number satisfying0<n≦4, preferably 2≦n≦4, more preferably 4.

The titanium compound represented by the general formula Ti(OR¹)_(n)X_(4-n) (0<n≦4) can be produced in accordance with known synthesisprocesses. For example, it can be produced in accordance with a processof reacting Ti(OR¹)₄ and TiX₄ in a given proportion or with a process ofreacting TiX₄ with a corresponding alcohol in a given proportion.

(b) Organo silicon compound having Si-O bonds

The organo silicon compound having Si-O bonds, used in the synthesis ofthe component (A) of the present catalyst system is represented by thefollowing general formula.

    Si(OR.sup.3).sub.m R.sup.4.sub.4-m'

    R.sup.5 (R.sup.6.sub.2 SiO)p SiR.sup.7.sub.3

    (R.sup.8.sub.2 SiO)q

(wherein R³ is a hydrocarbon group having 1 to 20 carbon atoms; R⁴, R⁵,R⁶, R⁷ and R⁸ are each a hydrocarbon group having 1 to 20 carbon atomsor a hydrogen atom; m is a number satisfying 0<m≦4; p is an integer of 1to 1,000; and q is an integer of 2 to 1,000).

Specific examples of the organo silicon compound include the followingcompounds.

Tetramethoxysilane, dimethyldimethoxysilane, tetraethoxysilane,triethoxyethylsilane, diethoxyethylsilane, ethoxytriethylsilane,tetraisopropoxysilane, diisopropoxydiisopropylsilane,tetrapropoxysilane, dipropoxydipropylsilane, tetra-n-butoxysilane,di-n-butoxy-di-n-butylsilane, dicyclopentoxydiethylsilane,diethoxydiphenylsilane, cyclohexyloxytrimethylsilane,phenoxytrimethylsilane, tetraphenoxysilane, triethoxyphenylsilane,hexamethyldisiloxane, hexaethyldisiloxane, hexapropyldisiloxane,octaethyltrisiloxane, dimethylpolysiloxane, diphenylpolysiloxane,methylhydropolysiloxane, and phenylhydropolysiloxane.

Preferably of these are alkoxysilane compounds represented by thegeneral formula Si(OR³)_(m) R⁴ _(4-m). The letter, m, is preferred to be1≦m≦4. A tetraalkoxysilane compound (m=4) is particularly preferred.

(c) Organo magnesium compound

The organo magnesium compound used in the present invention can be anyorgano magnesium compound as long as it has at least one Mg-C bond.There is preferably used a Grignard compound represented by the generalformula R⁹ MgX (wherein R⁹ is a hydrocarbon group having 1 to 20 carbonatoms and X is a halogen atom), or a dialkylmagnesium compound or adiarylmagnesium compound both represented by the general formula R¹⁰ R¹¹Mg (wherein P¹⁰ and R¹¹ are each a hydrocarbon group having 1 to 20carbon atoms). The symbols, R⁹, R¹⁰ and R¹¹ can be same or different andare each an alkyl, aryl, aralkyl or alkenyl group of 1 to 20 carbonatoms such as methyl, ethyl, n-propyl, isopropyl, n-butyl, sec-butyl,tert-butyl, n-amyl, isoamyl, n-hexyl, n-octyl, 2-ethylhexyl, phenyl,benzyl or the like.

Specific examples of the Grignard compound include methylmagnesiumchloride, ethylmagnesium chloride, ethylmagnesium bromide,ethylmagnesium iodie, n-propylmagnesium chloride, n-propylmagnesiumbromide, n-butylmagnesium chloride, n-butylmagnesium bromide,sec-butylmagnesium chloride, sec-butylmagnesium bromide,tert-butylmagnesium chloride, tert-butylmagnesium bromide,n-amylmagnesium chloride, isoamylmagnesium chloride, phenylmagnesiumchloride and phenylmagnesium bromide. Specific examples of the compoundrepresented by R¹⁰ R¹¹ Mg include diethylmagnesium,di-n-propylmagnesium, diisopropylmagnesium, di-n-butylmagnesium,di-sec-butylmagnesium, di-tert-butylmagnesium,n-butyl-sec-butylmagnesium, di-n-amylmagnesium and diphenylmagnesium.

As the synthesis solvent for the organo magnesium compound, there can beused an ether solvent such as diethyl ether, di-n-propyl ether,diisopropyl ether, di-n-butyl ether, diisobutyl ether, di-n-amyl ether,diisoamyl ether, di-n-hexyl ether, di-n-octyl ether, diphenyl ether,dibenzyl ether, phenetol, anisole, tetrahydrofuran, tetrahydropyran orthe like. Alternatively, there can be used a hydrocarbon solvent such ashexane, heptane, octane, cyclohexane, methylcyclohexane, benzene,toluene, xylene or the like, or a mixed solvent of an ether solvent anda hydrocarbon solvent. The organo magnesium compound is used preferablyin the form of ether solution. The ether in this case is an ethercompound having at least 6 carbon atoms within the molecule or having acyclic structure.

The use of a Grignard compound represented by R⁹ MgCl in the form of anether solution is particularly preferred from the point of catalystpotency.

The organo magnesium compound can also be used in the form of ahydrocarbon-soluble complex between said compound an organo metalcompound capable of rendering the organo magnesium compound soluble inhydrocarbons. Examples of the organo metal compound include organiccompounds of Li, Be, B, Al or Zn.

(d) Ether compound

As the ether compound of the present invention, there are preferablyused dialkyl ethers such as diethyl ether, di-n-propyl ether,diisopropyl ether, di-n-butyl ether, di-n-amyl ether, diisoamyl ether,dineopentyl ether, di-n-hexyl ether, di-n-octyl ether, methyl n-butylether, methyl isoamyl ether, ethyl isobutyl ether and the like.

Of these, di-n-butyl ether and diisoamyl ether are particularlypreferable.

(e) Synthesis of the solid catalyst component (A)

The solid catalyst component (A) of the present invention can besynthesized by reducing a titanium compound represented by the generalformula Ti(OR¹)_(n) X_(4-n) with an organo magnesium compound and thentreating the resulting solid product with a mixture of an ether compoundand titanium teterachloride.

Preferably, the reduction of the titanium compound with the organomagnesium compound is conducted in the presence of an organo siliconcompound having Si-O bonds.

All the steps of the synthesis reaction are conducted in an inert gasatmosphere such as nitrogen, argon or the like.

In the reduction of the titanium compound with the organo magnesiumcompound, the organo magnesium compound is added to a mixture of thetitanium compound and the organo silicon compound. Alternatively, saidmixture of the titanium compound and the organo silicon compound may beadded to a solution of the organo magnesium compound. In view of thecatalytic activity, a process comprising adding an organo magnesiumcompound to a mixture of a titanium compound and an organo siliconecompound is preferred.

Preferably, the titanium compound and the organo silicon compound areused after having been dissolved in or diluted by an appropriatesolvent.

As such a solvent, there can be mentioned aliphatic hydrocarbons such ashexane, heptane, octane, decane and the like; aromatic hydrocarbons suchas toluene, xylene, decalin and the like; alicyclic hydrocarbons such ascyclohexane, methylcyclohexane and the like; and ether compounds such asdiethyl ether, dibutyl ether, diisoamyl ether, tetrahydrofuran and thelike.

The reduction temperature is generally -50° to 70° C., preferably -30°to 50° C., and particularly preferably -25° to 35° C. If the reductiontemperature is excessively high, the catalytric activity lowers.

The dropping time has no particular restriction but ordinarily is 30minutes to about 6 hours. After the completion of the reduction, apost-reaction may be conducted at a temperature of 20° to 120° C.

The amount of the organo silicon compound used is 0 to 50, preferably 1to 30, particularly preferably 3 to 25 in terms of Si/Ti, namely, theatomic ratio of silicon atom to titanium atom in titanium compound.

The amount of the organo magnesium compound used is 0.1 to 10,preferably 0.2 to 5.0, particularly preferably 0.5 to 2.0 in terms of(Ti+Si)/Mg, namely, the atomic ratio of the sum of titanium atom andsilicon atom to magnesium atom.

The solid product obtained by the reduction is subjected to solid-liquidseparation and then washed several times with an inert hydrocarbonsolvent such as hexane, heptane or the like.

The solid product thus obtained contains trivalent titanium, magnesiumand hydrocarbyloxy group and is generally amorphous or very slightlycrystalline. Preferably, it has an amorphous structure from the point ofcatalyst potency.

The solid product is then treated with a mixture of an ether compoundand titanium tetrachloride.

The treatment of the solid product with a mixture of the ether compoundand titanium tetrachloride is preferably conducted in a slurry state.The solvent used for slurrying includes aliphatic hydrocarbons such aspentane, hexane, heptane, octane, decane and the like; aromatichydrocarbons such as toluene, xylene, decalin and the like; alicyclichydrocarbons such as cyclohexane, methylcyclohexane and the like; andhalogenated hydrocarbons such as dichlorethane, trichloroethane,trichloroethylene, monochlorobenzene, dichlorobenzene, trichlorobenzeneand the like.

The slurry concentration is preferably 0.05 to 0.5 g solid/ml solvent,particularly preferably 0.1 to 0.3 g solid/ml solvent.

The reaction temperature is 30 ° to 150° C., preferably 45° to 120° C.,particularly preferably 60° to 100° C.

The reaction time has no particular restriction but ordinarily is 30minutes to 6 hours.

With respect to the addition order of the solid product, the ethercompound and titanium tetrachloride, the ether compound and titaniumtetrachloride can be added to the solid product, or, the solid productcan be added to a solution containing both the ether compound andtitanium tetrachloride.

When the ether compound and titanium tetrachloride are added to thesolid product, it is preferably that the ether compound and titaniumtetrachloride be added separately in this order or simultaneously.

The reaction of the solid product with a mixture of the ether compoundand titanium tetrachloride can be conducted two times or more.

The amount of the ether compound used is 0.1 to 100 moles, preferably0.5 to 50 moles, particularly preferably 1 to 20 moles per 1 mole oftitanium atom in solid product.

The amount of titanium tetrachloride added is 1 to 1,000 moles,preferably 3 to 500 moles, particularly preferably 10 to 300 moles per 1mole of titanium atom in solid product. The amount of titaniumtetrachloride added is also 1 to 100 moles, preferably 1.5 to 75 moles,particularly preferably 2 to 50 moles per 1 mole of ether compound.

The thus obtained solid catalyst component containing a trivalenttitanium compound is subjected to solid-liquid separation. The resultingsolid is washed several times with an inert hydrocarbon solvent such ashexane, heptane or the like and then is used for polymerization ofolefins.

The solid obtained from the step of solid-liquid separation may bewashed with an excessive amount of a halogenated hydrocarbon solvent(e.g. monochlorobenzene) at least one time at a temperature of 50° to120° C., followed by several times of washing with an aliphatichydrocarbon solvent (e.g. hexane) and then be used for olefinpolymerization.

(f) Organo aluminum compound (B)

The organo aluminum compound (B) used in combination with the solidcatalyst component (A) in the present invention has a least one Al-Cbond in the molecule. The organo aluminum compound are typicallyrepresented by the following general formulas.

    R.sup.12.sub.γ  AlY.sub.3-γ

    or

    R.sup.13 R.sup.14 Al--O--AlR.sup.15 R.sup.16

(wherein R¹², R¹³, R¹⁴, R¹⁵ and R¹⁶ are each a hydrocarbon group having1 to 8 carbon atoms; Y is a halogen atom, a hydrogen atom or an alkoxygroup; and γ is a number satisfying 2≦γ≦3).

Specific examples of the organo aluminum compound includetrialkylaluminums such as triethylaluminum, triisobutylaluminum,trihexylaluminum and the like; dialkylaluminum hydrides such asdiethylaluminum hydride, diisobutylaluminum hydride and the like;dialkylaluminum halides such as diethylaluminum chloride and the like;mixtures between a trialkylaluminum and a dialkylaluminum halide; andalkyl alumoxanes such as tetraethyl dialumoxane, tetrabutyl dialumoxaneand the like.

Preferable of these organo aluminum compounds are trialkylaluminums,mixtures of a trialkylaluminum and a dialkylaluminum halide, and alkylalumoxanes. Particularly preferable are triethylaluminum,triisobutylaluminum, a mixture of triethylaluminum and diethylaluminumchloride, and tetraethyl dialumoxane.

The amount of the organo aluminum compound used can be selected aswidely as 1 to 1,000 moles per 1 mole of titanium atom in solidcatalyst. The amount preferably is 5 to 600 moles.

(g) Polymerization of olefins

Feeding of each catalyst component into a polymerization reactor can beconducted with no particular restriction except that the feeding isconducted in an inert gas such as nitrogen, argon or the like which isfree from moisture.

The catalyst components (A) and (B) can be fed separately, or, can becontacted with each other in advance before feeding.

The polymerization can be carried out at temperatures between -30° C.and 200° C.

The polymerization pressure has no particular restriction but desirablyis about 3 to 100 atm from industrial and economical standpoints. Thepolymerization can use a continuous method or a batch method. Also, thepolymerization can use a slurry polymerization method employing an inerthydrocarbon solvent such as propane, butane, pentane, hexane, heptane,octane or the like or a liquid phase or gas phase polymerization methodemploying no solvent.

The olefins usable in the present invention are those having 2 or morecarbon atoms. Specifically there can be mentioned ethylene, propylene,butene-1, pentene-1, hexane-1, 3-methylpentene-1, 4-methylpentene-1,etc. Needless to say, other olefins can be used in the presentinvention. The polymerization according to the present invention can behomopolymerization or copolymerization. In copolymerization, a mixtureof two or more different olefins is contacted with the present catalystsystem, whereby a copolymer is produced.

Heteroblock copolymerization wherein polymerization is conducted in twoor more stages can also be conducted easily with the present catalystsystem.

It is also possible to add a chain transfer agent such as hydrogen tothe polymerization system in order to control the molecular weight ofthe polymer obtained.

It is also possible to add a known electron-donating compound to thepolymerization system in order to improve the stereoregularity andmolecular weight of the polymer obtained. Typical examples of such anelectron-donating compound are organic carboxylic acid esters such asmethyl methacrylate, methyl toluate and the like; phosphorous acidesters such as triphenyl phosphite and the like; silicic acid esterssuch as tetraethoxysilane, phenyltriethoxysilane and the like.

The present invention will be explained in more detail below by way ofExamples and Comparative Examples but the invention is not limitedthereto.

EXAMPLE 1

(1) Synthesis or organo magnesium compound

A flask having an internal volume of 1 liter, equipped with a stirrer, areflux condenser, a dropping funnel and a thermometer was purged withargon. 32.0 g of chipped magnesium for Grignard reagent was placedtherein. 120 g of n-butyl chloride and 500 ml of di-n-butyl ether wereplaced in the dropping funnel and about 30 ml of the resulting mixturewas dropped into the flask to start a reaction with magnesium. Thisdropping was continued at 50° C. for 4 hours from the start of thereaction. After the termination of the dropping, the reaction wascontinued for further 1 hour at 60° C. Then, the reaction mixture wascooled down to room temperature and the solid portion was removed byfiltration.

N-Butylmagnesium chloride present in di-n-butyl ether was hydrolyzedwith 1N sulfuric acid and back-titrated with a 1N aqueous sodiumhydroxide solution using phenolphthalein as an indicator to determinethe concentration of n-butylmagnesium chloride. The concentration was2.03 moles per liter.

(2) Synthesis of solid product

A flask having an internal volume of 500 ml, equipped with a stirrer anda dropping funnel was purged with argon. Therein were placed 300 ml ofn-heptane, 31 g of tetrabutoxytitanium and 18 g of ethyl orthosilicate,and they were made into a uniform solution. Then, 100 ml of the organomagnesium compound prepared in the above (1), placed in the droppingfunnel of the flask was slowly dropped into the flask in 2 hours whilekeeping the temperature inside the flask at 5° C., to effect a reductionreaction. After the termination of the dropping, stirring was continuedfor further 1 hour at room temperature, after which the reaction mixturewas allowed to stand at room temperature to conduct solid-liquidseparation. The solid was washed three times with 300 ml of n-heptaneand then dried under vacuum to obtain a grayish brown solid product.

(3) Synthesis of solid catalyst component containing tri-valent titaniumcompound

A flask having an internal volume of 100 ml was purged with argon.Therein were placed 11.3 g of the solid product prepared in the above(2) and 56 ml of n-heptane. The temperature of the flask was kept at 80°C.

Thereto were added 7.6 ml of di-n-butyl ether and 29 ml of titaniumtetrachloride, and reaction was conducted at 80° C. for 1 hour.

The reaction mixture was allowed to stand at room temperature forsolid-liquid separation. The solid was washed four times with 50 ml ofn-heptane and dried under vacuum to obtain a solid catalyst component ofviolet color.

1 g of this solid catalyst component contained 2.6 mM of titanium, 5.5mM of magnesium, 0.27 mM of ethoxy group, 0.32 mM of butoxy group and0.69 mM of butyl ether.

(4) Polymerization of ethylene

An autoclave having an internal volume of 0.4 liter, equipped with astirrer was thoroughly purged with argon. Therein was placed 250 ml ofn-heptane. The autoclave was heated to 180° C. and ethylene was addeduntil the total pressure inside the autoclave became 12.5 kg/cm².Further, 20 mg of the solid catalyst component prepared in the above (3)and 1 mM of triethylaluminum were added to start a polymerization. Thepolymerization was conducted for 5 minutes at 180° C. while continuouslyfeeding ethylene to keep the total pressure at the above mentionedlevel. After the completion of the polymerization, the reaction mixturewas filtered to separate the polymer formed. The polymer was dried at60° C. under vacuum and 14.4 g of the polymer was gained. The catalyticactivities of the catalyst used were 719 g.polymer/g.solid catalyst and5,750 g.polymer/g.titanium.

COMPARATIVE EXAMPLE 1

A solid catalyst component was synthesized in the same procedure as inExample 1 except that di-n-butyl ether used in (3) synthesis of solidcatalyst component of Example 1 was not used. 1 g of this solid catalystcomponent contained 3.2 mM of titanium, 3.9 mM of magnesium, 0.82 mM ofethoxy group and 0.75 mM of butoxy group.

Using the above solid catalyst, ethylene was polymerized in the sameprocedure as in (4) of Example 1. The catalytic activities of thecatalyst used were 250 g.polymer/g.solid catalyst and 1,600g.polymer/g.titanium.

EXAMPLE 2

(1) Synthesis of solid product

A flask having an internal volume of 500 ml, equipped with a stirrer anda dropping funnel were purged with argon. Therein were placed 23 g oftetrabutoxytitanium, 52 g of ethyl orthosilicate and 310 ml of heptane,and they were made into a uniform solution. 150 ml of the organomagnesium compound synthesized in (1) of Example 1, placed in thedropping funnel of the flask was slowly dropped in 2 hours while keepingthe temperature inside the flask at 5° C., to effect a reductionreaction. After the completion of the dropping, stirring was continuedfor further 1 hour at room temperature. The reaction mixture was allowedto stand at room temperature for solid-liquid separation. The solid waswashed three times with 300 ml of n-heptane and dried under vacuum toobtain a grayish brown solid product.

1 g of this solid product contained 0.77 mM of tri-valent titanium, 6.2mM of magnesium, 7.0 mM of ethoxy group and 1.9 mM of butoxy group.

(2) Synthesis of solid catalyst component

The flask having an internal volume of 100 ml was purged with argon.Therein were placed 7.1 g of the solid product prepared in the above (1)and 30 ml of n-heptane. The temperature inside the flask was kept at 80°C. Then, 2.8 ml of di-n-butyl ether and 19 ml of titanium tetrachloridewere added and a reaction was conducted at 80° C. for 1 hour. Thereaction mixture was allowed to stand at room temperature forsolid-liquid separation. The solid was washed four times with 80 ml ofn-heptane and dried under vacuum to obtain a solid catalyst component ofviolet color.

1 g of this solid catalyst contained 2.7 mM of titanium, 5.1 mM ofmagnesium, 0.57 mM of ethoxy group and 0.19 mM of butoxy group.

(3) Polymerization of ethylene

Ethylene polymerization was conducted in the same procedure as inExample 1-(4) except that the solid catalyst component prepared in theabove (2) was used. The catalytic activities of the catalyst used were563 g.polymer/g.solid catalyst and 4,330 g.polyer/g.titanium.

EXAMPLE 3

A solid catalyst component was synthesized in the same procedure as inExample 2-(2) except that the amount of titanium tetrachloride usedchanged to 37 ml. 1 g of this solid catalyst component contained 2.7 mMof titanium, 5.4 mM of magnesium, 0.43 mM of ethoxy group and 0.16 mM ofbutoxy group. Using this solid catalyst component, ethylenepolymerization was conducted in the same procedure as in Example 1-(4).The catalytic activities of the catalyst used were 760 g.polymer/g.solidcatalyst and 5,890 g.polymer/g.titanium.

EXAMPLE 4

A solid catalyst component was synthesized in the same procedure as inExample 2-(2) except that the amount of titanium tetrachloride used waschanged to 55 ml. 1 g of this solid catalyst component contained 1.3 mMof titanium, 6.1 mM of magnesium, 0.46 mM of ethoxy group and 0.27 mM ofbutoxy group.

Using the above solid catalyst component, ethylene polymerization wasconducted in the same procedure as in Example 1-(4). The catalyticactivities of the catalyst used were 781 g.polymer/g.solid catalyst and9,170 g.polymer/g.titanium.

EXAMPLE 5

A solid catalyst component was synthesized in the same procedure as inExample 2-(2) except that the amount of di-n-butyl ether used changed to1.4 ml. 1 g of this solid catalyst component contained 2.9 mM oftitanium, 5.4 mM of magnesium, 0.61 mM of ethoxy group and 0.17 mM ofbutoxy group.

Using the above catalyst component, ethlene polymerization was conductedin the same procedure as in Example 1-(4). The catalytic activities ofthe catalyst used were 490 g.polymer/g.solid catalyst and 3,520g.polymer/g.titanium.

EXAMPLE 6

A solid catalyst component was synthesized in the same procedure as inExample 2-(2) except that the amount of di-n-butyl ether was changed to11 ml. 1 g of this solid catalyst component contained 1.4 mM oftitanium, 6.2 mM of magnesium, 0.16 mM of ethoxy group and 0.25 mM ofbutoxy group.

Using this catalyst component, ethylene polymerization was conducted inthe same procedure as in Example 1-(4). The catalytic activities of thecatalyst used were 854 g.polymer/g.solid catalyst and 12,700g.polymer/g.titanium.

EXAMPLE 7

A solid catalyst component was synthesized in the same procedure as inExample 2-(2) except that the amount of di-n-butyl ether used waschanged to 21 ml. 1 g of this solid catalyst component contained 0.75 mMof titanium, 8.4 mM of magnesium, 0.08 mM of ethoxy group and 0.06 mM ofbutoxy group.

Using this catalyst component, ethylene polymerization was conducted inthe same procedure as in Example 1-(4). The catalytic activities of thecatalyst used were 313 g.polymer/g.solid catalyst and 8,650g.polymer/g.titanium.

EXAMPLE 8

(1) Polymerization of ethylene

An autoclave having an internal volume of 0.4 liter, equipped with astirrer was purged thoroughly with argon. Therein were placed 200 ml ofn-heptane and 5 g of butene-1. The temperature of the autoclave wasincreased to 50° C. and ethylene was fed thereinto until the totalpressure inside the autoclave became 3.1 kg/cm². 2 mg of the solidcatalyst component prepared in Example 1 and 1 mM of triethylaluminumwere added, after which a polymerization was started. The polymerizationwas conducted at 50° C. for 1 hour while continuously feeding ethyleneto keep the total pressure at the above mentioned level. After thecompletion of the polymerization, the reaction mixture was filtered toseparate the polymer formed. The polymer was dried at 60° C. undervacuum. The catalytic activities of the catalyst used were 24,200g.polymer/g.solid catalyst and 164,000 g.polymer/g.titanium.

COMPARATIVE EXAMPLE 2

Ethylene polymerization was conducted in the same procedure as inExample 8 except that the solid catalyst component prepared inComparative Example 1 was used in Comparative Example 2. The catalyticactivities of the catalyst used were, in this case, 18,600g.polymer/g.solid catalyst and 121,000 g.polymer/g.titanium.

EXAMPLE 9

(1) Synthesis of solid product

A flask having an internal volume of 500 ml, equipped with a stirrer anda dropping funnel was purged with argon. Therein were placed 34 g oftetrabutoxytitanium and 210 ml of heptane, and they were made into auniform solution., 50 ml of the organo magnesium compound prepared inExample 1-(1), placed in the dropping funnel of the flask was slowlydropped in 2 hours while keeping the temperature inside the flask at 5°C., to effect a reduction reaction. After the completion of thedropping, stirring was continued for further 1 hour at room temperature.The reaction mixture was allowed to stand at room temperature forsolid-liquid separation. The solid was washed three times with 300 ml ofn-heptane and dried under vacuum to obtain a blackish brown solidproduct.

1 g of this solid contained 1.9 mM of tri-valent titanium, 1.7 mM ofmagnesium and 7.2 mM of butoxy group.

(2) Synthesis of solid catalyst component containing tri-valent titaniumcompound.

A flask having an internal volume of 100 ml was purged with argon.Therein were placed 9.3 g of the solid product prepared in the above (1)and 39 ml of n-heptane. The temperature inside the flask was kept at 80°C.

Then, 4.7 ml of diisoamyl ether and 50 ml of titanium tetrachloride wereadded and a reaction was conducted at 80° C. for 1 hour.

The reaction mixture was allowed to stand at room temperature forsolid-liquid separation. The solid was washed four times with 50 ml ofn-heptane and dried under vacuum to obtain a solid catalyst component ofviolet color.

1 g of this solid catalyst component contained 2.9 mM of titanium, 3.1mM of magnesium, 0.27 mM of butoxy group and 0.41 mM of diisoamyl ether.

(3) Polymerization of ethylene

An autoclave having an internal volume of 0.4 liter, equipped with astirrer was purged with argon thoroughly. Therein were added 200 ml ofcyclohexane and 10 g of butene-1. The temperature inside the autoclavewas increased to 230° C. and ethylene was fed into the autoclave untilthe total pressure inside the autoclave became 39.0 kg/cm². Then, 30 mgof the solid catalyst component prepared in the above (2) and 1 mM oftriethylaluminum were added to start a polymerization. Thepolymerization was conducted at 230° C. for 2 minutes while continuouslyfeeding ethylene to keep the total pressure at the above mentionedlevel. After the completion of the polymerization, the polymer formedwas separated by filtration and dried at 60° C. under vacuum. Thecatalytic activities of the catalyst used were 96 g.polymer/g.solidcatalyst and 700 g.polymer/g.titanium.

EXAMPLE 10

(1) Synthesis of solid catalyst component containing tri-valent titaniumcompound

By using 10 g of the solid product prepared in Example 9-(1) and byadding diisoamyl ether and titanium tetrachloride, a reaction wasconducted in the same procedure as in Example 9-(2). The reactionproduct was separated and washed with n-heptane. The resulting productwas subjected to two more times of reaction with diisoamyl ether andtitanium tetrachloride. 1 g of the solid catalyst component thusobtained contained 2.7 mM of titanium, 3.9 mM of magnesium, 0.03 mM ofbutoxy group and 0.53 mM of diisoamyl ether.

(2) Polymerization of ethylene

Ethylene polymerization was conducted in the same procedure as inExample 9-(3) except that the solid catalyst component prepared in theabove (1) was used. THe catalytic activities of the catalyst used were113 g.polymer/solid catalyst and 860 g.polymer/g.titanium.

EXAMPLE 11

Ethylene polymerization was conducted in the same procedure as inExample 9-(3) except that the solid catalyst component prepared inExample 10-(1) was used and triethylaluminum was replaced by 1 mM ofdiethylaluminum chloride. The catalytic activities of the catalyst usedwere 347 g.polymer/g.solid catalyst and 2,650 g.polymer/g.titanium.

EXAMPLE 12

(1) Polymerization of propylene

A stainless steel autoclave of magnetic stirring type, having aninternal volume of 130 ml was purged with argon. Therein were placed0.57 mM of triethylaluminum, 0.057 mM of ethyl phenylsilicate, 10 mg ofthe solid catalyst component prepared in Example 1 and 80 ml ofliquefied propylene.

The autoclave contents were kept at 60° C. for 1 hour with stirring.Excessive propylene was released. The polypropylene formed was air-driedfor 24 hours. The catalytic activity of the catalyst used was 1,500g.polymer/g.solid catalyst.

The percentage of insolubles when the polypropylene powder obtained wassubjected to 6 hours extraction with boiling n-heptane (hereinafter thispercentage is abbreviated to "IY") was 81.9%.

COMPARATIVE EXAMPLE 3

Propylene polymerization was conducted in the same procedure as inExample 12 except that the solid catalyst component of ComparativeExample 1 was used. The catalytic activity of the catalyst used was 710g.polymer/g.solid catalyst. IY was 73.6%.

As appreciated from the above explanation, the catalyst system of thepresent invention has very high catalytic activities not only per solidcatalyst but also per titanium atom. Hence, polymers produced with saidcatalyst system, without employing any special procedure for catalystresidue removal, are very low in halogen atom and titanium atom contentswhich greatly affect the coloring, stability and corrosiveness ofpolymers. This requires no facility for catalyst residue removal and canreduce the production cost of olefin polymers.

What is claimed is:
 1. A process for producing olefin polymers whichcomprises homopolymerizing or copolymerizing olefins in the presence ofa catalyst system comprising:(A) A solid catalyst component containing atrivalent titanium compound, which is obtained by reducing a titaniumcompound represented by the general formula Ti(OR¹)_(n) X_(4-n) (whereinR¹ is a hydrocarbon group having 1 to 20 carbon atoms, X is a halogenatom and n is a number satisfying 0<n≦4) with an organo magnesiumcompound in the presence of an organo silicon compound having Si-O bondsrepresented by the following formula:

    Si(OR.sup.3).sub.m R.sup.4.sub.4-m,

    R.sup.5 (R.sup.6.sub.2 SiO).sub.p SiR.sup.7.sub.3

    or

    (R.sup.8.sub.2 SiO)q

(wherein R³ is a hydrocarbon group having 1 to 20 carbon atoms; R⁴, R⁵,R⁶, R⁷ and R⁸ are each a hydrocarbon group having 1 to 20 carbon atomsor a hydrogen atom; m is a number satisfying 0<n≦4); p is an integer of1 to 1,000; and q is an integer of 2 to 1,000), and then treating theresulting solid product with a mixture of dialkyl ether and titaniumtetrachloride, and (B) an organo aluminum compound, at a temperature of-30° C. to 200°C. under a pressure of 3 to 100 atm.
 2. A process forproducing olefin polymers according to claim 1, wherein R¹ is ahydrocarbon group having 2 to 18 carbon atoms.